CA2284854C - Circulating fluidized bed reactor with floored internal primary particle separator - Google Patents
Circulating fluidized bed reactor with floored internal primary particle separator Download PDFInfo
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- CA2284854C CA2284854C CA002284854A CA2284854A CA2284854C CA 2284854 C CA2284854 C CA 2284854C CA 002284854 A CA002284854 A CA 002284854A CA 2284854 A CA2284854 A CA 2284854A CA 2284854 C CA2284854 C CA 2284854C
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- floor
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- flue gas
- particle separators
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- 239000011164 primary particle Substances 0.000 title abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 147
- 239000002245 particle Substances 0.000 claims abstract description 141
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 68
- 239000003546 flue gas Substances 0.000 claims abstract description 68
- 238000011144 upstream manufacturing Methods 0.000 claims description 13
- 239000007789 gas Substances 0.000 description 7
- 238000002485 combustion reaction Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000010276 construction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/04—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia
- B01D45/08—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by utilising inertia by impingement against baffle separators
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0065—Separating solid material from the gas/liquid stream by impingement against stationary members
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
- B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
- B07B7/00—Selective separation of solid materials carried by, or dispersed in, gas currents
- B07B7/04—Selective separation of solid materials carried by, or dispersed in, gas currents by impingement against baffle separators
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/20—Intercepting solids by baffles
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A CFB reactor or combustor having an impact type primary particle separator collects solids particles from a flow of flue gas/solids and returns the collected particles along an inclined or substantially horizontal planar floor to a bottom portion of the reactor or combustor for subsequent recirculation.
Description
Case 60IfZ
CIRCULATING FLUIDIZED BED REACTOR WITH
FLOORED INTERNAL PRIMARY PARTICLE SEPARATOR
FIELD OF THE INVENTION
The present invention relates, in general, to circulating fluidized bed (CFB) reactors or combustors having impact type particle separators and, more particularly, to a CFB reactor or combustor having an improved impact type primary particle separator. Instead of providing a cavity means or hopper with discharge openings underneath the collector elements making up the impact type primary particle separator, a simple floor provides for internal return of all primary collected solids to a bottom portion of the reactor or combustor for subsequent recirculation.
BACgGROUND OF THE INVENTION
In CFB reactors or combustors, reacting and non-reacting solids are entrained within a reactor enclosure by an upward gas flow which carries the solids to an exit at an upper portion of the reactor enclosure. There, the solids are typically collected by an impact type primary particle separator, and returned to a bottom portion of the reactor enclosure either directly or through one or more conduits. The impact type primary particle separator at the reactor enclosure exit typically collects from 90% to 97% of the circulating solids.
lff required by the process, an additional solids collector may be installed downstream of the impact type primary particle separator to collect additional solids for eventual return to the reactor enclosure.
As disclosed in U.S. Patent No. 5,343,830 to Alexander et al., the use of impact type particle separators in CFB reactors or combustors is well known. To the extent necessary~to describe the.general operation of CFB reactors and combustors, the reader is.
referred to U.S.
Patent No. 5,343,830 to Alexander et al. In one of the earliest CI'iB designs, an external, impact type p~~' p~lcle separator having a plurality of impingement members arranged in staggered rows was used in combination with a non-mechanical-L-valve and a secondary {multiclone) particle separator. The rows of staggered impingement members discharged all of their collected solids into a storage hopper located underneath them, and these collected solids were returned to the bottom portion of the reactor enclosure via the L-valve.
Later CFB designs employed additional rows of staggered impingement members which were positioned upstream (with respect to a direction of flue gas and solids flow through the apparatus) of the impingement members associated with the storage hopper and its L-valve. As disclosed in U.S. Patent No. 4,992,085 to Belie et al., a plurality of such impingement members are located within an upper portion of the reactor enclosure, arranged in at least two staggered rows.
The ~Pingement members hang and extend vertically across a width of the reactor exit, with collectedsolids falling unobstructed and unchanneled underneath these collecting impingement.
members along a rear enclosure wall of the CFB reactor or combustor. An important element of these "in-furnace" collecting impingement members, or "in-furnace U-bes~tns" as they are generally referred to, is a baffle plate near a lower end of these impingement members which educes their collection efficiency.
As disclosed in the aforementioned Alexander et al. '830 patent, CFB reactors or combustors are lmown wherein the two or more rows of impingement members located within the furnace or reactor enclosure are followed by a second array of staggered impingement Case 60b2 members which further separate particles from the gas stream, and return them via cavity means and particle return means without external and internal recycle conduits.
It is apparent that a CFB reactor or combustor comprising an even more simple construction would be less costly and would be welcomed by industry.
FIELD OF THE INVENTION
The present invention relates generally to the field of circulating fluidized bed (CFB) reactors or combustors and provides a simpler and lower cost impact type primary particle separator. In particular, instead of providing a cavity means or hopper with discharge openings underneath the collector elements making up the impact type primary particle separator, a simple floor provides for internal return of all primary collected solids to a bottom portion of the reactor or combustor for subsequent recirculation.
In its simplest form, the present invention comprises two or more rows of staggered impact type particle separators whose lower ends extend to or proximate to a simple, substantially planar floor. The floor can be inclined towards the reactor enclosure, towards a downstream direction with respect to a flow of flue gas/solids through the CFB, in both directions, or even horizontal. The impact type particle separators operate in known fashion, collecting solids from the flue gas/solids flowing through a passage or flue containing the impact type particle separators and conducting them to their lower ends. These collected solids are then rcmoved by gravity from the flue by one of the following modes.
If the floor is inclined at some angle with respect to horizontal so that the floor is sloped towards a reactor enclosure of the CFB, the separated solids particles will slide down the floor and into the reactor enclosure along a rear enclosure wail thereof. If the floor is inclined so that it is downward sloping towards a downstream direction with respect to a flow of flue gas/solids thmugh the passage or flue, the separated solids particles will slide down the floor in the direction of flue gas/solids flow where they can be collected in a downstream cavity, hopper, or removal trough for collection and eventual return to a bottom portion of the reactor enclosure.
In some cases, the floor may be provided with a peak to facilitate solids particles sliding down both towards the reactor enclosure and towards a downstream direction. In any event, the floor's Case 60Y2 angle of inclination, a, will generally be selected so that it is equal to or greater than the angle of repose aR for such separated solids.
However, the concept of the present invention is also applicable even if the floor is horizontal. The separated solids collected by the particle separators will begin to build up into a pile on such a horizontal floor until a slope of the pile reaches the angle of repose aR for such separated solids, at which point the solids will then begin to slide down along the pile, either towards the reactor enclosure or in the direction of flue gas/solids flow.
Particles sliding down the floor back towards the reactor enclosure are directly returned for subsequent recirculation, while particles sliding down the floor in the direction of flue gas/solids flow will be collected in a cavity, hopper, or removal trough for collection and eventual return to a bottom portion of the reactor enclosure.
In cases where the collected solids particles flow down towards the reactor enclosure, a flue gas/solids deflector means can be used to increase the fraction of collected solids particles which slide down the floor and into the reactor enclosure along the rear enclosure wall. In cases where the collected solids particles flow in the direction of flue gas/solids flow, deflector means may or may not be used to enhance the flow of separated solids particles along the floor to the downstream cavity, hopper, or removal trough.
The floored internal impact type primary particle separator according to the present invention can be used with or without the upstream, in-furnace U-beams.
Accordingly one aspect of the present invention is drawn to an improved CFB
reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB
reactor, comprising: a reactor enclosure having an exit opening; a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids; a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening; and a floor located below the second group of particle separators.
Another aspect of the present invention is drawn to an improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing thmugh a reactor enclosure of the CFB
reactor, Case 6012 comprising: a reactor enclosure having an exit opening; a group of at least two rows of staggered impact type particle separators located downstream of the exit opening with respect to the flow of flue gas/solids; and a floor located below the group of particle separators.
Yet still another aspect of the present invention is drawn to an improved CFB
reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB
reactor, comprising: a reactor enclosure having an exit opening; at least two rows of staggered impact type particle separators, at least one row located upstream of the exit opening and at least one row located downstream of the exit opening with respect to the flow of flue gas/solids; and a floor located below the at least one row of particle separators located downstream of the exit opening.
The various features of novelty which characterize the invention are pointed out with particularity in the claims annexed to and forming a part of this disclosure.
For a better understanding of the invention, its operating advantages and spxific benefits attained by its uses, reference is made to the accompanying drawings and descriptive matter in which a preferred embodiment of the invention is illustrated.
BRIEF DESCRIPTION OF THE DRAWINGS
In the drawings:
Fig. 1 is a schematic sectional side elevation view of a portion of a circulating fluidized bed (CFB) reactor or combustor according to a first embodiment of the invention;
Fig. 2 is a schematic sectional plan view of Fig. 1 viewed in the direction of arrows 2-2;
Fig. 3 is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a second embodiment of the invention;
Fig. 4 is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a third embodiment of the invention;
Fig. 5 is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a fourth embodiment of the invention;
Case 6022 Fig. 5A is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a fifth embodiment of the invention;
Fig. 6 is a schematic sectional side elevation view of a first embodiment of a gas/solids deflector means which may be used in the CFB reactor or combustor at a lower end of the staggered impact type particle separator elements;
Fig. 7 is a schematic sectional plan view of Fig. 6 taken in the direction of arrows 7-7, the U-beams 140 being omitted for clarity;
Fig. 8 is a schematic sectional side view of a second embodiment of a gas/solids deflector means which may be used at a lower end of the staggered impact type particle separator elements; and Fig. 9 is a schematic sectional plan view of Fig. 8 taken in the direction of arrows 9-9.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
As used herein, the term CFB combustor refers to a type of CFB reactor where a combustion process takes place. While the present invention is directed particularly to boilers or steam generators which employ CFB combustors as the means by which the heat is produced, it is understood that the present invention can readily be employed in a different kind of CFB
reactor. For example, the invention could be applied in a reactor that is employed for chemical reactions other than a combustion process, or where a gas/solids mixture from a combustion pmcess occurring elsewhere is provided to the reactor for further processing, or where the reactor merely provides an enclosure wherein particles or solids are entrained in a gas that is not necessarily a byproduct of a combustion process.
Referring generally to the drawings, wherein like reference numerals represent the same or functionally similar elements throughout the several drawings, and to Figs.
1 and 2 in particular, there is shown a circulating fluidized bed (CFB) reactor or combustor, generally designated 10, comprising a reactor enclosure 20 having an upper portion 30, an exit opening 40, and a convection pass 50. The front of the CFB reactor enclosure is defined as the left hand side of Figs. 1 and 2; the rear is the right hand sides of these Figs, and the width of the CFB
reactor enclosure 20 is perpendicular to the plane of Fig. 1. The reactor enclosure 20 is typically rectangular in cross-section and is defined by enclosure walls 100. Enclosure walls 100 are COse 601.2 usually fluid cooled, being typically comprised of water and/or steam conveying tubes separated from one another by a steel membrane to achieve a gas-tight reactor enclosure 20. A flue gas/solids mixture 110 produced by the CFB combustion process occurring in a lower portion of the reactor enclosure 20 flows upwardly through the upper portion 30 and eventually out the exit opening 40 and into the convection pass 50. As the flue gas/solids mixture 110 travels along this path, it passes across several solids particle and heat removal stages, as will be herein described, before being passed to the atmosphere.
Located in the upper portion 30 of the reactor enclosure 20, in the direction of the flue gas/solids flow 110 and upstream of the exit opening 40, is a first group 130 (one or more rows, preferably two rows) of staggered impact type particle separators 140. The particle separators 140 are non-planar, they may be U-shaped, E-shaped, W-shaped or any other shape which presents a cupped or concave surface configuration to the flow of incoming flue gas/solids 110.
As described earlier, since the first group 130 of impact type particle separators are upstream of the exit opening 40, this first group 130 may also be referred to as the in-furnace U-beams 130.
For the sake of convenience, the staggered impact type particle separators 140 will be generally referred to in the balance of the description as U-beams 140. The U-beams 140 are staggered with respect to one another such that the flue gas/solids flow 110 passes through them enabling the entrained solids particles to strike them and be collected in their cupped or concave portion, and causing the collected particles (generally referred to as 150, regardless of which separator elements 140 collect them) collected by the first group 130 to free fall internally and directly down along the U-beams towards a bottom portion of the reactor enclosure 20. U-beams 140 also extend fully across the exit opening 40. U-beams 140 are typically made of stainless steel due to the high temperature environment.
Positioned just dovvnsheam of the exit opening 40 is a second group 160 of impact type particle separators or U-beams 140, (also referred to as the primary impact type particle separators 160). The U-beams 140 in this second group 160 of at least two rows of staggered impact type particle separators (preferably 4 rows), located downstream of the exit opening 40, also collect particles 150 from the flue gas/solids flow 110. However, in contrast to the known arrangements wherein lower ends 170 of such U-beams 140 making up the second group 160 extend into a cavity below them which is used to temporarily collect and return collected solids Case 602 _g_ particles back to the reactor enclosure 20, the CFB reactor 10 according to the present invention is merely provided with a floor 180 having no apertures or openings therein for particles to fall through.
As illustrated in Fig. 3, the floored internal impact type primary particle separator 160 according to the present invention can be used without the upstream group of in-furnace U-beams 130, but it is preferred that they be employed to enhance solids particles 150 collection efficiency. Similarly, while at least two rows of staggered impact type particle separators or U-beams 140 are required, the at least two rows can be located dovvnsbream of the exit opening 40, or at least one row can be located upstream of the exit opening 40 and at least one mw can be located downstream of the exit opening 40.
Floor 180 may be and is preferably inclined so that collected solids particles 150 slide along floor 180 towards the reactor enclosure 20. However, floor 180 may be substantially horizontal as illustrated in Fig. 4, or it may be inclined so that collected solids particles 150 slide along floor 180 in the direction of flue gas/solids flow 110 where they can be collected in a downstream cavity, hopper or trough 190 as illustrated in Fig. 5 for collection and eventual return to a bottom portion of the reactor enclosure. If desired, floor 180 may even be provided with a peak 182 such that it has not only a first portion 184 inclined so that collected solids particles 150 slide along floor 180 towards the reactor enclosure 20, but also a second portion 186 inclined so that collected solids particles 150 slide along floor 180 in the direction of flue gas/solids flow 110 where they can be collected in the downstream cavity, hopper or trough 190 as illustrated in Fig. 5A for collection and eventual return to a bottom portion of the reactor enclosure. In any event, where floor 180 is inclined, floor 180's angle of inclination, a, will generally be selected so that it is equal to or greater than the angle of repose aR for such separated solids. Floor 180 is preferably substantially planar in construction, but if it is inclined it may be provided with a series of channels or grooves therein along which collected solids particles 150 may flow or slide.
The floored impact type particle separator concept of the present invention is also applicable even if the floor 180 is horizontal or substantially horizontal (Fig. 4). The separated solids 150 collected by the second group of particle separators 160 will begin to build up into a pile on such a horizontal floor 180 until a slope of the pile reaches the angle of repose aR for Case 6012 such separated solids 1 S0, at which point the solids 1 SO will then begin to slide down along the pile, either towards the reactor enclosure 20 or in the direction of flue gas/solids flow 110.
Particles 1 SO sliding down the floor 180 back towards the reactor enclosure 20 are directly returned for subsequent recirculation, while particles 1S0 sliding down the floor 180 in the direction of flue gas/solids flow 180 will be collected in the downstream cavity, hopper, or removal trough 190 for collection and eventual return to a bottom portion of the reactor enclosure 20.
In cases where the collected solids particles 1S0 flow down the floor 180 towards the reactor enclosure 20, a flue gas/solids deflector means can be used to increase the fiaction of collected solids particles which slide down the floor 180 and into the reactor enclosure 20 along the rear enclosure wall 200. In cases where the collected solids particles 1S0 flow in the direction of flue gas/solids flow 110, deflector means may or may not be used to enhance the flow of separated solids particles 180 along the floor 180 to the downstream cavity, hopper, or removal trough 190.
Referring to Figs. 6 and 7, one embodiment of the flue gas/solids deflector means, generally referred to as 250, comprises a plate 260 having a lip 270 at an upper portion thereof, a substantially horizontal baffle 280 extending from the plate 260, and standoff means 290 for securing the plate 260 to the rear wall 200 of the reactor enclosure 20.
Preferably the flue gas/solids deflector means is positioned at a location proximate to an intersection of the floor 180 and the rear enclosure wall 200.
Referring to Figs. 8 and 9, another embodiment of the flue gas/solids deflector means merely employs an arrangement of plate 300, 310 secured, such as by welding, to lower ends of both the in-furnace U-beams 140 and the U-beams 140 comprising the second group of particle separators 160. As illustrated, a continuous plate 300 might be placed at the front of the first in-filmace U-beams 140, while separate plates 310 might be employed at the rear of successive U-beams 140.
The U-beams 140 making up the second group 160 are preferably the same design as those comprising the first group 130 and preferably extend to the floor 180, but consideration must be given to the fact that the U-beams 140 could expand or "grow"
downwardly as the operating temperature in the CFB reactor increases. Providing clearance between the lower ends Case 6012 170 of the U-beams 140 comprising the second group 1b0 and the floor 180 is one way to prevent contact during operation. However, if that approach is desired or acceptable, a balance must be struck between providing adequate clearance and too much clearance because the collected solids particles 150 could bypass the lower ends 170 of the U-beams 140, resulting in their not being returned to the reactor enclosure 20 for subsequent recirculation. Alternatively, cooling of such U-beams 140 might be provided to minimize or control such thermal expansion during operation, such as but not limited to the use of indirect cooling as disclosed in U.S. Patent No. 5,809,940 to James et al., or by providing cooled U-beam 140 structures such as but not limited to those disclosed in U.S. Patent Nos. 5,378,253 and 5,435,820 to Daum et al. Still further, a floor 180 or roof 210 structure could be employed which fixes one end of the U-beam 140 and allows for a "slip-fit" at the other, or which allows for movement at both ends, or if contact is determined to be relatively unobjectionable, a floor 180 structure wherein the U-beams 140 touch and/or are actually embedded in the floor 180 could be employed.
Some of the reactor enclosure tubes 100 which form a rear wall 200 of the reactor enclosure 20 extend upwardly towards a roof 210 of the convection pass 50 to form what is referred to in the art as a "screen" at the exit opening 40. The fluid-cooled tubes forming this screen are generally laterally spaced apart from one another, forming gas lanes (not shown) through which the flue gas/solids 110 flows. The floor 180 is typically cooled, and it may be formed by some of the fluid-cooled enclosure tubes 100 or by other fluid-cooled tubes.
With reference again to Figs. 1 and 2, and continuing through the convection pass 50 in the direction of flue gas/solids 110 flow, banks of tubes comprising heating surfaces such as superheater, reheater, boiler (water/steam), or even economizer surface, schematically shown in Figs. 1 and 2 as 220 and 230, may be provided. The flue gas/solids 110 passing across these banks of tubes 220, 230 gives up a portion of the heat contained therein to the working fluid within the tubes comprising these tube banks 220, 230 to achieve the thermodynamic work required by any steam turbine or other process (not shown) associated with the CFB reactor or combustor 10. After passing across these banks of tubes 220, 230, the flue gas/solids flow 110 may be provided to further downstream heating surfaces (not shown) and to additional particulate collection devices (also not shown).
Ciese 6012 The present invention minimizes or eliminates the inefficiencies caused by gas-bypass-induced reentrainment of solids through a discharge hopper or cavity located beneath the primary impact type particle separators 160. 'This means that additional rows of U-beams 140 may be added in this group 160, beyond the 4 or 5 rows typically employed, to increase particle collection effciency.
Further, the configurations of Figs. 4, 5 and SA can be used where it is desirable to remove the collected solids 150 from the process or to route the collected solids back to the reactor enclosure 20 via an external conduit (not shown) or possibly to external devices such as an external fluidized bed heat exchanger (also not shown).
While a specific embodiment of the invention has been shown and descn'bed in detail to illustrate the application of the principles of the invention, it will be understood that the invention may be embodied otherwise without departing from such principles.
For example, the present invention may be applied to new constmction involving CFB reactors or combustors, or to the repair, replacement, or modification of existing CFB reactors or combustors. In some embodiments of the invention, certain features of the invention may be used to advantage without a corresponding use of other features. Accordingly, all such changes embodiments properly fall within the scope and equivalents of the following claims.
CIRCULATING FLUIDIZED BED REACTOR WITH
FLOORED INTERNAL PRIMARY PARTICLE SEPARATOR
FIELD OF THE INVENTION
The present invention relates, in general, to circulating fluidized bed (CFB) reactors or combustors having impact type particle separators and, more particularly, to a CFB reactor or combustor having an improved impact type primary particle separator. Instead of providing a cavity means or hopper with discharge openings underneath the collector elements making up the impact type primary particle separator, a simple floor provides for internal return of all primary collected solids to a bottom portion of the reactor or combustor for subsequent recirculation.
BACgGROUND OF THE INVENTION
In CFB reactors or combustors, reacting and non-reacting solids are entrained within a reactor enclosure by an upward gas flow which carries the solids to an exit at an upper portion of the reactor enclosure. There, the solids are typically collected by an impact type primary particle separator, and returned to a bottom portion of the reactor enclosure either directly or through one or more conduits. The impact type primary particle separator at the reactor enclosure exit typically collects from 90% to 97% of the circulating solids.
lff required by the process, an additional solids collector may be installed downstream of the impact type primary particle separator to collect additional solids for eventual return to the reactor enclosure.
As disclosed in U.S. Patent No. 5,343,830 to Alexander et al., the use of impact type particle separators in CFB reactors or combustors is well known. To the extent necessary~to describe the.general operation of CFB reactors and combustors, the reader is.
referred to U.S.
Patent No. 5,343,830 to Alexander et al. In one of the earliest CI'iB designs, an external, impact type p~~' p~lcle separator having a plurality of impingement members arranged in staggered rows was used in combination with a non-mechanical-L-valve and a secondary {multiclone) particle separator. The rows of staggered impingement members discharged all of their collected solids into a storage hopper located underneath them, and these collected solids were returned to the bottom portion of the reactor enclosure via the L-valve.
Later CFB designs employed additional rows of staggered impingement members which were positioned upstream (with respect to a direction of flue gas and solids flow through the apparatus) of the impingement members associated with the storage hopper and its L-valve. As disclosed in U.S. Patent No. 4,992,085 to Belie et al., a plurality of such impingement members are located within an upper portion of the reactor enclosure, arranged in at least two staggered rows.
The ~Pingement members hang and extend vertically across a width of the reactor exit, with collectedsolids falling unobstructed and unchanneled underneath these collecting impingement.
members along a rear enclosure wall of the CFB reactor or combustor. An important element of these "in-furnace" collecting impingement members, or "in-furnace U-bes~tns" as they are generally referred to, is a baffle plate near a lower end of these impingement members which educes their collection efficiency.
As disclosed in the aforementioned Alexander et al. '830 patent, CFB reactors or combustors are lmown wherein the two or more rows of impingement members located within the furnace or reactor enclosure are followed by a second array of staggered impingement Case 60b2 members which further separate particles from the gas stream, and return them via cavity means and particle return means without external and internal recycle conduits.
It is apparent that a CFB reactor or combustor comprising an even more simple construction would be less costly and would be welcomed by industry.
FIELD OF THE INVENTION
The present invention relates generally to the field of circulating fluidized bed (CFB) reactors or combustors and provides a simpler and lower cost impact type primary particle separator. In particular, instead of providing a cavity means or hopper with discharge openings underneath the collector elements making up the impact type primary particle separator, a simple floor provides for internal return of all primary collected solids to a bottom portion of the reactor or combustor for subsequent recirculation.
In its simplest form, the present invention comprises two or more rows of staggered impact type particle separators whose lower ends extend to or proximate to a simple, substantially planar floor. The floor can be inclined towards the reactor enclosure, towards a downstream direction with respect to a flow of flue gas/solids through the CFB, in both directions, or even horizontal. The impact type particle separators operate in known fashion, collecting solids from the flue gas/solids flowing through a passage or flue containing the impact type particle separators and conducting them to their lower ends. These collected solids are then rcmoved by gravity from the flue by one of the following modes.
If the floor is inclined at some angle with respect to horizontal so that the floor is sloped towards a reactor enclosure of the CFB, the separated solids particles will slide down the floor and into the reactor enclosure along a rear enclosure wail thereof. If the floor is inclined so that it is downward sloping towards a downstream direction with respect to a flow of flue gas/solids thmugh the passage or flue, the separated solids particles will slide down the floor in the direction of flue gas/solids flow where they can be collected in a downstream cavity, hopper, or removal trough for collection and eventual return to a bottom portion of the reactor enclosure.
In some cases, the floor may be provided with a peak to facilitate solids particles sliding down both towards the reactor enclosure and towards a downstream direction. In any event, the floor's Case 60Y2 angle of inclination, a, will generally be selected so that it is equal to or greater than the angle of repose aR for such separated solids.
However, the concept of the present invention is also applicable even if the floor is horizontal. The separated solids collected by the particle separators will begin to build up into a pile on such a horizontal floor until a slope of the pile reaches the angle of repose aR for such separated solids, at which point the solids will then begin to slide down along the pile, either towards the reactor enclosure or in the direction of flue gas/solids flow.
Particles sliding down the floor back towards the reactor enclosure are directly returned for subsequent recirculation, while particles sliding down the floor in the direction of flue gas/solids flow will be collected in a cavity, hopper, or removal trough for collection and eventual return to a bottom portion of the reactor enclosure.
In cases where the collected solids particles flow down towards the reactor enclosure, a flue gas/solids deflector means can be used to increase the fraction of collected solids particles which slide down the floor and into the reactor enclosure along the rear enclosure wall. In cases where the collected solids particles flow in the direction of flue gas/solids flow, deflector means may or may not be used to enhance the flow of separated solids particles along the floor to the downstream cavity, hopper, or removal trough.
The floored internal impact type primary particle separator according to the present invention can be used with or without the upstream, in-furnace U-beams.
Accordingly one aspect of the present invention is drawn to an improved CFB
reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB
reactor, comprising: a reactor enclosure having an exit opening; a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids; a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening; and a floor located below the second group of particle separators.
Another aspect of the present invention is drawn to an improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing thmugh a reactor enclosure of the CFB
reactor, Case 6012 comprising: a reactor enclosure having an exit opening; a group of at least two rows of staggered impact type particle separators located downstream of the exit opening with respect to the flow of flue gas/solids; and a floor located below the group of particle separators.
Yet still another aspect of the present invention is drawn to an improved CFB
reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB
reactor, comprising: a reactor enclosure having an exit opening; at least two rows of staggered impact type particle separators, at least one row located upstream of the exit opening and at least one row located downstream of the exit opening with respect to the flow of flue gas/solids; and a floor located below the at least one row of particle separators located downstream of the exit opening.
The various features of novelty which characterize the invention are pointed out with particularity in the claims annexed to and forming a part of this disclosure.
For a better understanding of the invention, its operating advantages and spxific benefits attained by its uses, reference is made to the accompanying drawings and descriptive matter in which a preferred embodiment of the invention is illustrated.
BRIEF DESCRIPTION OF THE DRAWINGS
In the drawings:
Fig. 1 is a schematic sectional side elevation view of a portion of a circulating fluidized bed (CFB) reactor or combustor according to a first embodiment of the invention;
Fig. 2 is a schematic sectional plan view of Fig. 1 viewed in the direction of arrows 2-2;
Fig. 3 is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a second embodiment of the invention;
Fig. 4 is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a third embodiment of the invention;
Fig. 5 is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a fourth embodiment of the invention;
Case 6022 Fig. 5A is a schematic sectional side elevation view of a portion of a CFB
reactor or combustor according to a fifth embodiment of the invention;
Fig. 6 is a schematic sectional side elevation view of a first embodiment of a gas/solids deflector means which may be used in the CFB reactor or combustor at a lower end of the staggered impact type particle separator elements;
Fig. 7 is a schematic sectional plan view of Fig. 6 taken in the direction of arrows 7-7, the U-beams 140 being omitted for clarity;
Fig. 8 is a schematic sectional side view of a second embodiment of a gas/solids deflector means which may be used at a lower end of the staggered impact type particle separator elements; and Fig. 9 is a schematic sectional plan view of Fig. 8 taken in the direction of arrows 9-9.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
As used herein, the term CFB combustor refers to a type of CFB reactor where a combustion process takes place. While the present invention is directed particularly to boilers or steam generators which employ CFB combustors as the means by which the heat is produced, it is understood that the present invention can readily be employed in a different kind of CFB
reactor. For example, the invention could be applied in a reactor that is employed for chemical reactions other than a combustion process, or where a gas/solids mixture from a combustion pmcess occurring elsewhere is provided to the reactor for further processing, or where the reactor merely provides an enclosure wherein particles or solids are entrained in a gas that is not necessarily a byproduct of a combustion process.
Referring generally to the drawings, wherein like reference numerals represent the same or functionally similar elements throughout the several drawings, and to Figs.
1 and 2 in particular, there is shown a circulating fluidized bed (CFB) reactor or combustor, generally designated 10, comprising a reactor enclosure 20 having an upper portion 30, an exit opening 40, and a convection pass 50. The front of the CFB reactor enclosure is defined as the left hand side of Figs. 1 and 2; the rear is the right hand sides of these Figs, and the width of the CFB
reactor enclosure 20 is perpendicular to the plane of Fig. 1. The reactor enclosure 20 is typically rectangular in cross-section and is defined by enclosure walls 100. Enclosure walls 100 are COse 601.2 usually fluid cooled, being typically comprised of water and/or steam conveying tubes separated from one another by a steel membrane to achieve a gas-tight reactor enclosure 20. A flue gas/solids mixture 110 produced by the CFB combustion process occurring in a lower portion of the reactor enclosure 20 flows upwardly through the upper portion 30 and eventually out the exit opening 40 and into the convection pass 50. As the flue gas/solids mixture 110 travels along this path, it passes across several solids particle and heat removal stages, as will be herein described, before being passed to the atmosphere.
Located in the upper portion 30 of the reactor enclosure 20, in the direction of the flue gas/solids flow 110 and upstream of the exit opening 40, is a first group 130 (one or more rows, preferably two rows) of staggered impact type particle separators 140. The particle separators 140 are non-planar, they may be U-shaped, E-shaped, W-shaped or any other shape which presents a cupped or concave surface configuration to the flow of incoming flue gas/solids 110.
As described earlier, since the first group 130 of impact type particle separators are upstream of the exit opening 40, this first group 130 may also be referred to as the in-furnace U-beams 130.
For the sake of convenience, the staggered impact type particle separators 140 will be generally referred to in the balance of the description as U-beams 140. The U-beams 140 are staggered with respect to one another such that the flue gas/solids flow 110 passes through them enabling the entrained solids particles to strike them and be collected in their cupped or concave portion, and causing the collected particles (generally referred to as 150, regardless of which separator elements 140 collect them) collected by the first group 130 to free fall internally and directly down along the U-beams towards a bottom portion of the reactor enclosure 20. U-beams 140 also extend fully across the exit opening 40. U-beams 140 are typically made of stainless steel due to the high temperature environment.
Positioned just dovvnsheam of the exit opening 40 is a second group 160 of impact type particle separators or U-beams 140, (also referred to as the primary impact type particle separators 160). The U-beams 140 in this second group 160 of at least two rows of staggered impact type particle separators (preferably 4 rows), located downstream of the exit opening 40, also collect particles 150 from the flue gas/solids flow 110. However, in contrast to the known arrangements wherein lower ends 170 of such U-beams 140 making up the second group 160 extend into a cavity below them which is used to temporarily collect and return collected solids Case 602 _g_ particles back to the reactor enclosure 20, the CFB reactor 10 according to the present invention is merely provided with a floor 180 having no apertures or openings therein for particles to fall through.
As illustrated in Fig. 3, the floored internal impact type primary particle separator 160 according to the present invention can be used without the upstream group of in-furnace U-beams 130, but it is preferred that they be employed to enhance solids particles 150 collection efficiency. Similarly, while at least two rows of staggered impact type particle separators or U-beams 140 are required, the at least two rows can be located dovvnsbream of the exit opening 40, or at least one row can be located upstream of the exit opening 40 and at least one mw can be located downstream of the exit opening 40.
Floor 180 may be and is preferably inclined so that collected solids particles 150 slide along floor 180 towards the reactor enclosure 20. However, floor 180 may be substantially horizontal as illustrated in Fig. 4, or it may be inclined so that collected solids particles 150 slide along floor 180 in the direction of flue gas/solids flow 110 where they can be collected in a downstream cavity, hopper or trough 190 as illustrated in Fig. 5 for collection and eventual return to a bottom portion of the reactor enclosure. If desired, floor 180 may even be provided with a peak 182 such that it has not only a first portion 184 inclined so that collected solids particles 150 slide along floor 180 towards the reactor enclosure 20, but also a second portion 186 inclined so that collected solids particles 150 slide along floor 180 in the direction of flue gas/solids flow 110 where they can be collected in the downstream cavity, hopper or trough 190 as illustrated in Fig. 5A for collection and eventual return to a bottom portion of the reactor enclosure. In any event, where floor 180 is inclined, floor 180's angle of inclination, a, will generally be selected so that it is equal to or greater than the angle of repose aR for such separated solids. Floor 180 is preferably substantially planar in construction, but if it is inclined it may be provided with a series of channels or grooves therein along which collected solids particles 150 may flow or slide.
The floored impact type particle separator concept of the present invention is also applicable even if the floor 180 is horizontal or substantially horizontal (Fig. 4). The separated solids 150 collected by the second group of particle separators 160 will begin to build up into a pile on such a horizontal floor 180 until a slope of the pile reaches the angle of repose aR for Case 6012 such separated solids 1 S0, at which point the solids 1 SO will then begin to slide down along the pile, either towards the reactor enclosure 20 or in the direction of flue gas/solids flow 110.
Particles 1 SO sliding down the floor 180 back towards the reactor enclosure 20 are directly returned for subsequent recirculation, while particles 1S0 sliding down the floor 180 in the direction of flue gas/solids flow 180 will be collected in the downstream cavity, hopper, or removal trough 190 for collection and eventual return to a bottom portion of the reactor enclosure 20.
In cases where the collected solids particles 1S0 flow down the floor 180 towards the reactor enclosure 20, a flue gas/solids deflector means can be used to increase the fiaction of collected solids particles which slide down the floor 180 and into the reactor enclosure 20 along the rear enclosure wall 200. In cases where the collected solids particles 1S0 flow in the direction of flue gas/solids flow 110, deflector means may or may not be used to enhance the flow of separated solids particles 180 along the floor 180 to the downstream cavity, hopper, or removal trough 190.
Referring to Figs. 6 and 7, one embodiment of the flue gas/solids deflector means, generally referred to as 250, comprises a plate 260 having a lip 270 at an upper portion thereof, a substantially horizontal baffle 280 extending from the plate 260, and standoff means 290 for securing the plate 260 to the rear wall 200 of the reactor enclosure 20.
Preferably the flue gas/solids deflector means is positioned at a location proximate to an intersection of the floor 180 and the rear enclosure wall 200.
Referring to Figs. 8 and 9, another embodiment of the flue gas/solids deflector means merely employs an arrangement of plate 300, 310 secured, such as by welding, to lower ends of both the in-furnace U-beams 140 and the U-beams 140 comprising the second group of particle separators 160. As illustrated, a continuous plate 300 might be placed at the front of the first in-filmace U-beams 140, while separate plates 310 might be employed at the rear of successive U-beams 140.
The U-beams 140 making up the second group 160 are preferably the same design as those comprising the first group 130 and preferably extend to the floor 180, but consideration must be given to the fact that the U-beams 140 could expand or "grow"
downwardly as the operating temperature in the CFB reactor increases. Providing clearance between the lower ends Case 6012 170 of the U-beams 140 comprising the second group 1b0 and the floor 180 is one way to prevent contact during operation. However, if that approach is desired or acceptable, a balance must be struck between providing adequate clearance and too much clearance because the collected solids particles 150 could bypass the lower ends 170 of the U-beams 140, resulting in their not being returned to the reactor enclosure 20 for subsequent recirculation. Alternatively, cooling of such U-beams 140 might be provided to minimize or control such thermal expansion during operation, such as but not limited to the use of indirect cooling as disclosed in U.S. Patent No. 5,809,940 to James et al., or by providing cooled U-beam 140 structures such as but not limited to those disclosed in U.S. Patent Nos. 5,378,253 and 5,435,820 to Daum et al. Still further, a floor 180 or roof 210 structure could be employed which fixes one end of the U-beam 140 and allows for a "slip-fit" at the other, or which allows for movement at both ends, or if contact is determined to be relatively unobjectionable, a floor 180 structure wherein the U-beams 140 touch and/or are actually embedded in the floor 180 could be employed.
Some of the reactor enclosure tubes 100 which form a rear wall 200 of the reactor enclosure 20 extend upwardly towards a roof 210 of the convection pass 50 to form what is referred to in the art as a "screen" at the exit opening 40. The fluid-cooled tubes forming this screen are generally laterally spaced apart from one another, forming gas lanes (not shown) through which the flue gas/solids 110 flows. The floor 180 is typically cooled, and it may be formed by some of the fluid-cooled enclosure tubes 100 or by other fluid-cooled tubes.
With reference again to Figs. 1 and 2, and continuing through the convection pass 50 in the direction of flue gas/solids 110 flow, banks of tubes comprising heating surfaces such as superheater, reheater, boiler (water/steam), or even economizer surface, schematically shown in Figs. 1 and 2 as 220 and 230, may be provided. The flue gas/solids 110 passing across these banks of tubes 220, 230 gives up a portion of the heat contained therein to the working fluid within the tubes comprising these tube banks 220, 230 to achieve the thermodynamic work required by any steam turbine or other process (not shown) associated with the CFB reactor or combustor 10. After passing across these banks of tubes 220, 230, the flue gas/solids flow 110 may be provided to further downstream heating surfaces (not shown) and to additional particulate collection devices (also not shown).
Ciese 6012 The present invention minimizes or eliminates the inefficiencies caused by gas-bypass-induced reentrainment of solids through a discharge hopper or cavity located beneath the primary impact type particle separators 160. 'This means that additional rows of U-beams 140 may be added in this group 160, beyond the 4 or 5 rows typically employed, to increase particle collection effciency.
Further, the configurations of Figs. 4, 5 and SA can be used where it is desirable to remove the collected solids 150 from the process or to route the collected solids back to the reactor enclosure 20 via an external conduit (not shown) or possibly to external devices such as an external fluidized bed heat exchanger (also not shown).
While a specific embodiment of the invention has been shown and descn'bed in detail to illustrate the application of the principles of the invention, it will be understood that the invention may be embodied otherwise without departing from such principles.
For example, the present invention may be applied to new constmction involving CFB reactors or combustors, or to the repair, replacement, or modification of existing CFB reactors or combustors. In some embodiments of the invention, certain features of the invention may be used to advantage without a corresponding use of other features. Accordingly, all such changes embodiments properly fall within the scope and equivalents of the following claims.
Claims (38)
1. An improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB reactor, comprising:
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located in a passage downstream of the exit opening, the flue gas/solids flowing through the passage; and a floor of the passage for returning particles collected from the flow of flue gas/solids, the floor located below the second group of particle separators.
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located in a passage downstream of the exit opening, the flue gas/solids flowing through the passage; and a floor of the passage for returning particles collected from the flow of flue gas/solids, the floor located below the second group of particle separators.
2. The improved CFB reactor or combustor arrangement of claim 1, wherein the floor is inclined at an angle with respect to horizontal so that the floor is sloped towards the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the floor towards the reactor enclosure.
3. The improved CFB reactor or combustor arrangement of claim 1, wherein the floor is inclined at an angle with respect to horizontal so that the floor is sloped towards a downstream direction with respect to the flow of flue gas/solids through the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the floor in the downstream direction.
4. The improved CFB reactor or combustor arrangement of claim 3, further comprising means for receiving collected solids particles which slide down the floor in the downstream direction.
5. The improved CFB reactor or combustor arrangement of claim 4, wherein the means for receiving collected solids particles comprises one of a cavity, hopper, and removal trough.
6. The improved CFB reactor or combustor arrangement of claim 1, wherein the floor is substantially horizontal.
7. The improved CFB reactor or combustor arrangement of claim 1, wherein the floor is substantially planar.
8. The improved CFB reactor or combustor of claim 1, wherein the floor is inclined at an angle a with respect to horizontal.
9. The improved CFB reactor or combustor of claim 8, wherein the angle a of inclination of the floor is equal to or greater than an angle of repose aR of the collected solid particles.
10. The improved CFB reactor or combustor of claim 8, wherein the floor is provided with one of a series of channels and grooves along which collected solids particles may flow or slide.
11. The improved CFB reactor or combustor arrangement of claim 8, further comprising flue gas/solids deflector means associated with the particle separators to reduce reentrainment of collected solids particles.
12. The improved CFB reactor or combustor arrangement of claim 11, wherein the flue gas/solids deflector means comprises a plate having a lip at an upper portion thereof, a substantially horizontal baffle extending from the plate, and standoff means for securing the plate to a rear wall of the reactor enclosure at a location proximate to an intersection of the floor and the rear enclosure wall.
13. The improved CFB reactor or combustor arrangement of claim 11, wherein the flue gas/solids deflector means comprises an arrangement of plate secured to lower ends of the impact type particle separators.
14. The improved CFB reactor or combustor arrangement of claim 1, further comprising a convection pass and heat transfer surface located therein.
15. The improved CFB reactor or combustor arrangement of claim 14, wherein the heat transfer surface comprises at least one of superheater surface, reheater surface, boiler surface and economizer surface.
16. The improved CFB reactor or combustor arrangement of claim 1, wherein the impact type particle separators comprise U-beams.
17. The improved CFB reactor or combustor arrangement of claim 1, wherein the impact type particle separators comprise non-planar elements which are U-shaped, E-shaped, W-shaped or any other shape which presents a cupped or concave surface configuration to the flow of flue gas/solids.
18. The improved CFB reactor or combustor arrangement of claim 1, wherein the floor is provided with a peak such that it is provided with a first portion inclined at a:n angle with respect to horizontal so that the floor is sloped towards the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the first portion of the floor towards the reactor enclosure, and a second portion inclined at an angle with respect to horizontal so that the floor is sloped towards a downstream direction with respect to the flow of flue gas/solids through the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the second portion of the floor in the downstream direction.
19. An improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB reactor, comprising:
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located in a passage downstream of the exit opening with respect to the flow of flue gas/solids through the passage; and a floor of the passage for returning particles collected from the flow of flue gas/solids, the floor located below the group of particle separators.
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located in a passage downstream of the exit opening with respect to the flow of flue gas/solids through the passage; and a floor of the passage for returning particles collected from the flow of flue gas/solids, the floor located below the group of particle separators.
20. An improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB reactor, comprising:
a reactor enclosure having an exit opening;
at least two rows of staggered impact type particle separators, at least one row located upstream of the exit opening and at least one row located in a passage downstream of the exit opening with respect to the flow of flue gas/solids through the passage; and a floor of the passage for returning particles collected from the flow of flue gas/solids, the floor located below the at least one row of particle separators located downstream of the exit opening.
a reactor enclosure having an exit opening;
at least two rows of staggered impact type particle separators, at least one row located upstream of the exit opening and at least one row located in a passage downstream of the exit opening with respect to the flow of flue gas/solids through the passage; and a floor of the passage for returning particles collected from the flow of flue gas/solids, the floor located below the at least one row of particle separators located downstream of the exit opening.
21. The improved CFB reactor or combustor arrangement of claims 19 or 20, wherein the floor is inclined at an angle with respect to horizontal so that the floor is sloped towards the reactor enclosure to cause solids particles collected by the particle separators to slide doom the floor towards the reactor enclosure.
22. The improved CFB reactor or combustor arrangement of claim l9 or 20, wherein the floor is inclined at an angle with respect to horizontal so that the floor is sloped towards a downstream direction with respect to the flow of flue gas/solids through the reactor enclosure to cause solids particles collected by the particle separators to slide down the floor in the downstream direction.
23. The improved CFB reactor or combustor arrangement of claim 22, further comprising one of a cavity, hopper, and removal trough means for receiving collected solids particles which slide down the floor in the downstream direction.
24. The improved CFB reactor or combustor arrangement of claims 19 or 20, wherein the floor is substantially horizontal.
25. The improved CFB reactor or combustor arrangement of claims 19 or 20, wherein the floor is substantially planar.
26. The improved CFB reactor or combustor of claims 19 or 20, wherein the floor is inclined at an angle .alpha. with respect to horizontal.
27. The improved CFB reactor or combustor of claim 26, wherein the angle .alpha. of inclination of the floor is equal to or greater than an angle of repose .alpha.R of the collected solids particles.
28. The improved CFB reactor or combustor of claim 26, wherein the floor is provided with one of a series of channels and grooves along which collected solids particles may flow or slide.
29. The improved CFB reactor or combustor arrangement of claim 26, further comprising flue gas/solids deflector means associated with the particle separators to reduce reentrainment of collected solids particles.
30. The improved CFB reactor or combustor arrangement of claim 29, wherein the flue gas/solids deflector means comprises a plate having a lip at an upper portion thereof, a substantially horizontal baffle extending from the plate, and standoff means for securing the plate to a rear wall of the reactor enclosure at a location proximate to an intersection of the floor and the rear enclosure wall.
31. The improved CFB reactor or combustor arrangement of claim 29, wherein the flue gas/solids deflector means comprises an arrangement of plate secured to lower ends of the impact type particle separators.
32. The improved CFB reactor or combustor arrangement of claims 19 or 20, further comprising a convection pass and at least one of superheater surface, reheater surface, boiler surface and economizer surface located therein.
33. The improved CFB reactor or combustor arrangement of claims 19 or 20, wherein the impact type particle separators comprise U-beams.
34. The improved CFB reactor or combustor arrangement of claim 33, wherein the impact type particle separators comprise non-planar elements which are U-shaped, E-shaped, W-shaped or any other shape which presents a cupped or concave surface configuration to the flow of flue gas/solids.
35. The improved CFB reactor or combustor arrangement of claims 19 or 20, wherein the floor is provided with a peak such that it is provided with a first portion inclined at an angle with respect to horizontal so that the floor is sloped towards the reactor enclosure to cause solids particles collected by the particle separators to slide down the first portion of the floor towards the reactor enclosure, and a second portion inclined at an angle with respect to horizontal so that the floor is sloped towards a downstream direction with respect to the flow of flue gas/solids through the reactor enclosure to cause solids particles collected by the particle separators to slide down the second portion of the floor in the downstream direction.
36. An improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB reactor, comprising:
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening; and a floor located below the second group of particle separators, wherein the floor is provided with a peak such that it is provided with a first portion inclined at an angle with respect to horizontal so that the floor is sloped towards the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the first portion of the floor towards the reactor enclosure, and a second portion inclined at an. angle with respect to horizontal so that the floor is sloped towards a downstream direction with the respect to the flow of flue gas/solids through the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the second portion of t:he floor in the downstream direction.
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening; and a floor located below the second group of particle separators, wherein the floor is provided with a peak such that it is provided with a first portion inclined at an angle with respect to horizontal so that the floor is sloped towards the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the first portion of the floor towards the reactor enclosure, and a second portion inclined at an. angle with respect to horizontal so that the floor is sloped towards a downstream direction with the respect to the flow of flue gas/solids through the reactor enclosure to cause solids particles collected by the second group of particle separators to slide down the second portion of t:he floor in the downstream direction.
37. An improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB reactor, comprising:
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening;
a floor inclined at an angle a with respect to horizontal located below the second group of particle separators; and flue gas/solids deflector means associated with the particle separators to reduce reentrainment of collected solids particles, wherein the flue gas/solids deflector means includes a plate having a lip at an upper portion thereof, a substantially horizontal baffle extending from the plate, and standoff means for securing the plate to a rear wall of the reactor enclosure at a location proximate to an intersection of the floor and the rear enclosure wall.
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exit opening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening;
a floor inclined at an angle a with respect to horizontal located below the second group of particle separators; and flue gas/solids deflector means associated with the particle separators to reduce reentrainment of collected solids particles, wherein the flue gas/solids deflector means includes a plate having a lip at an upper portion thereof, a substantially horizontal baffle extending from the plate, and standoff means for securing the plate to a rear wall of the reactor enclosure at a location proximate to an intersection of the floor and the rear enclosure wall.
38. An improved CFB reactor or combustor arrangement having impact type particle separators for separating solids particles from a flow of flue gas/solids flowing through a reactor enclosure of the CFB reactor, comprising:
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exitopening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening;
a floor inclined at an angle a with respect to horizontal located below the second group of particle separators; and flue gas/solids deflector means associated with the particle separators to reduce reentrainment of collected solids particles, wherein the flue gas/solids deflector means includes an arrangement of plate secured to lower ends of the impact type particle separators.
a reactor enclosure having an exit opening;
a group of at least two rows of staggered impact type particle separators located upstream of the exitopening with respect to the flow of flue gas/solids;
a second group of at least two rows of staggered impact type particle separators located downstream of the exit opening;
a floor inclined at an angle a with respect to horizontal located below the second group of particle separators; and flue gas/solids deflector means associated with the particle separators to reduce reentrainment of collected solids particles, wherein the flue gas/solids deflector means includes an arrangement of plate secured to lower ends of the impact type particle separators.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US09/206,353 | 1998-12-07 | ||
| US09/206,353 US6095095A (en) | 1998-12-07 | 1998-12-07 | Circulating fluidized bed reactor with floored internal primary particle separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2284854A1 CA2284854A1 (en) | 2000-06-07 |
| CA2284854C true CA2284854C (en) | 2003-09-09 |
Family
ID=22765988
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002284854A Expired - Fee Related CA2284854C (en) | 1998-12-07 | 1999-10-05 | Circulating fluidized bed reactor with floored internal primary particle separator |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US6095095A (en) |
| KR (1) | KR20000047628A (en) |
| CN (1) | CN1138090C (en) |
| BG (1) | BG64105B1 (en) |
| CA (1) | CA2284854C (en) |
| CZ (1) | CZ302226B6 (en) |
| ES (1) | ES2185438B2 (en) |
| PL (1) | PL196725B1 (en) |
| PT (1) | PT102386B (en) |
| RU (1) | RU2249764C2 (en) |
| UA (1) | UA58555C2 (en) |
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| CA2383170C (en) * | 2001-05-25 | 2007-10-30 | The Babcock & Wilcox Company | Cooled tubes arranged to form impact type particle separators |
| ES2305274T3 (en) * | 2001-06-29 | 2008-11-01 | Keppel Seghers Holdings Pte Ltd | COMBUSTION GAS PURIFICATION DEVICE FOR AN INCINERATOR. |
| US6681722B1 (en) * | 2002-10-18 | 2004-01-27 | The Babcock & Wilcox Company | Floored impact-type solids separator using downward expanding separator elements |
| US7828876B2 (en) * | 2007-04-20 | 2010-11-09 | Southern Company | Systems and methods for organic particulate filtration |
| US9163830B2 (en) * | 2009-03-31 | 2015-10-20 | Alstom Technology Ltd | Sealpot and method for controlling a solids flow rate therethrough |
| US8187369B2 (en) * | 2009-09-18 | 2012-05-29 | General Electric Company | Sorbent activation plate |
| CN103776013B (en) * | 2012-10-24 | 2016-03-02 | 中国石油化工股份有限公司 | There is the CO boiler of dusting function |
| CN103776014B (en) * | 2012-10-24 | 2015-11-18 | 中国石油化工股份有限公司 | A kind of CO boiler with dusting function |
| JP2017141997A (en) * | 2016-02-08 | 2017-08-17 | 三菱日立パワーシステムズ株式会社 | Fluidized bed boiler |
| US9989244B2 (en) * | 2016-03-01 | 2018-06-05 | The Babcock & Wilcox Company | Furnace cooling by steam and air injection |
| US11207627B2 (en) | 2018-10-17 | 2021-12-28 | University Of Kentucky Research Foundation | Filter assembly and scrubber section for a continuous miner |
| CN109443054A (en) * | 2018-12-19 | 2019-03-08 | 济南鲍德炉料有限公司日照市分公司 | Annular lime kiln air heat exchanger |
| WO2023183310A2 (en) * | 2022-03-21 | 2023-09-28 | Azul 3D, Inc. | Three dimensional printing process flow management and support systems |
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- 1998-12-07 US US09/206,353 patent/US6095095A/en not_active Expired - Lifetime
-
1999
- 1999-10-05 CA CA002284854A patent/CA2284854C/en not_active Expired - Fee Related
- 1999-11-05 ES ES9902430A patent/ES2185438B2/en not_active Expired - Lifetime
- 1999-11-12 KR KR1019990050237A patent/KR20000047628A/en not_active Application Discontinuation
- 1999-12-03 CN CNB991258703A patent/CN1138090C/en not_active Expired - Lifetime
- 1999-12-03 RU RU99125837/06A patent/RU2249764C2/en active
- 1999-12-06 PL PL336972A patent/PL196725B1/en unknown
- 1999-12-06 CZ CZ0437699A patent/CZ302226B6/en not_active IP Right Cessation
- 1999-12-06 UA UA99126625A patent/UA58555C2/en unknown
- 1999-12-06 PT PT102386A patent/PT102386B/en not_active IP Right Cessation
- 1999-12-07 BG BG103961A patent/BG64105B1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| PT102386A (en) | 2000-06-30 |
| UA58555C2 (en) | 2003-08-15 |
| RU2249764C2 (en) | 2005-04-10 |
| BG103961A (en) | 2000-07-31 |
| BG64105B1 (en) | 2003-12-31 |
| PL336972A1 (en) | 2000-06-19 |
| KR20000047628A (en) | 2000-07-25 |
| CA2284854A1 (en) | 2000-06-07 |
| PL196725B1 (en) | 2008-01-31 |
| CZ302226B6 (en) | 2011-01-05 |
| CZ9904376A3 (en) | 2001-03-14 |
| US6095095A (en) | 2000-08-01 |
| PT102386B (en) | 2002-02-28 |
| CN1256962A (en) | 2000-06-21 |
| CN1138090C (en) | 2004-02-11 |
| ES2185438A1 (en) | 2003-04-16 |
| ES2185438B2 (en) | 2012-06-14 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20171005 |